CA2928613A1 - Reclaiming device, method, and recovery unit of co2, h2s, or both of co2 and h2s - Google Patents
Reclaiming device, method, and recovery unit of co2, h2s, or both of co2 and h2s Download PDFInfo
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- CA2928613A1 CA2928613A1 CA2928613A CA2928613A CA2928613A1 CA 2928613 A1 CA2928613 A1 CA 2928613A1 CA 2928613 A CA2928613 A CA 2928613A CA 2928613 A CA2928613 A CA 2928613A CA 2928613 A1 CA2928613 A1 CA 2928613A1
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- vapor
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- absorbent
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- 238000011084 recovery Methods 0.000 title claims abstract description 44
- 238000000034 method Methods 0.000 title claims description 22
- 239000007788 liquid Substances 0.000 claims abstract description 99
- 239000002250 absorbent Substances 0.000 claims abstract description 93
- 230000002745 absorbent Effects 0.000 claims abstract description 93
- 239000000126 substance Substances 0.000 claims abstract description 85
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 77
- 238000010521 absorption reaction Methods 0.000 claims abstract description 41
- 238000000926 separation method Methods 0.000 claims abstract description 26
- 238000010438 heat treatment Methods 0.000 claims abstract description 10
- 239000007789 gas Substances 0.000 claims description 62
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 37
- 239000003546 flue gas Substances 0.000 claims description 37
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 31
- 238000001816 cooling Methods 0.000 claims description 30
- 239000006096 absorbing agent Substances 0.000 claims description 28
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 15
- 238000010992 reflux Methods 0.000 claims description 14
- 238000009835 boiling Methods 0.000 claims description 9
- 229910052757 nitrogen Inorganic materials 0.000 claims description 5
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 4
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 177
- 229910002092 carbon dioxide Inorganic materials 0.000 description 88
- 239000000243 solution Substances 0.000 description 46
- 238000010586 diagram Methods 0.000 description 22
- MWUXSHHQAYIFBG-UHFFFAOYSA-N Nitric oxide Chemical compound O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 9
- 239000000498 cooling water Substances 0.000 description 7
- 230000000694 effects Effects 0.000 description 7
- 150000001412 amines Chemical class 0.000 description 6
- 230000003247 decreasing effect Effects 0.000 description 5
- 238000002485 combustion reaction Methods 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 3
- 238000006477 desulfuration reaction Methods 0.000 description 3
- 230000023556 desulfurization Effects 0.000 description 3
- TXKMVPPZCYKFAC-UHFFFAOYSA-N disulfur monoxide Inorganic materials O=S=S TXKMVPPZCYKFAC-UHFFFAOYSA-N 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 230000001172 regenerating effect Effects 0.000 description 3
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical compound S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 239000003463 adsorbent Substances 0.000 description 2
- 239000007864 aqueous solution Substances 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 239000002803 fossil fuel Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 238000010792 warming Methods 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 238000010525 oxidative degradation reaction Methods 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 229910052815 sulfur oxide Inorganic materials 0.000 description 1
- 230000001629 suppression Effects 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/96—Regeneration, reactivation or recycling of reactants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1462—Removing mixtures of hydrogen sulfide and carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1468—Removing hydrogen sulfide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1475—Removing carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1493—Selection of liquid materials for use as absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/343—Heat recovery
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/52—Hydrogen sulfide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/52—Hydrogen sulfide
- B01D53/526—Mixtures of hydrogen sulfide and carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/62—Carbon oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/16—Hydrogen sulfides
- C01B17/167—Separation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/30—Alkali metal compounds
- B01D2251/304—Alkali metal compounds of sodium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/604—Hydroxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/204—Amines
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/204—Amines
- B01D2252/20478—Alkanolamines
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
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- Environmental & Geological Engineering (AREA)
- Biomedical Technology (AREA)
- Health & Medical Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Sustainable Development (AREA)
- Gas Separation By Absorption (AREA)
- Treating Waste Gases (AREA)
- Carbon And Carbon Compounds (AREA)
Abstract
Provided are a reclaimer 51 that introduces, through a branch line L11, and stores a part 17a of an absorbent 17 regenerated in a regenerator of a recovery unit that recovers CO2 or H2S in a gas, a first alkaline agent supply section 53A that supplies an alkaline agent 52 to the reclaimer 51, a heating section 54 that heats the absorbent 17 stored in the reclaimer 51 and to which the alkaline agent 52 has been mixed to obtain recovered vapor 61, a first vapor cooler 55A that cools the recovered vapor 61 discharged from the reclaimer 51 through a vapor line L12, a first gas-liquid separator 56A that separates a coexisting substance 62 entrained in the cooled recovered vapor 61 into a recovered absorption agent vapor (gas) 17b and the liquid coexisting substance 62 by gas-liquid separation, and an introduction line L13 that introduces the recovered absorption agent vapor 17b separated in the first gas-liquid separator 56A into a regenerator 20.
Description
Docket No. PMHA-16014-PCT
DESCRIPTION
RECLAIMING DEVICE, METHOD, AND RECOVERY UNIT OF CO2, H2S, Field [0001] The present invention relates to a reclaiming device, a method, and a recovery unit of CO2, H25, or both of CO2 and H2S.
Background
DESCRIPTION
RECLAIMING DEVICE, METHOD, AND RECOVERY UNIT OF CO2, H2S, Field [0001] The present invention relates to a reclaiming device, a method, and a recovery unit of CO2, H25, or both of CO2 and H2S.
Background
[0002] In recent years, as a cause of global warming of the earth, the greenhouse effect due to CO2 has been pointed out, and measures against the greenhouse effect is internationally imperative in terms of protection of the earth environment. Generation sources of CO2 extend over every field of human activities that burn fossil fuels, and demands for suppression of emission of CO2 tends to increase. In response to the demands, a method of bringing a flue gas in a boiler in contact with an amine-based CO2 absorbent such as an alkanolamine aqueous solution, and removing and recovering CO2 in the flue gas, and a method of storing the recovered CO2 without emitting CO2 to the air have been vigorously studied for power generation facilities such as thermal power stations that use a large amount of fossil fuels.
[0003] Conventionally, Patent Literature 1 discloses a method of removing CO2 (carbon dioxide) and SOx (sulfur oxide) in a flue gas. This method includes a denitrification process of reducing NOx (nitrogen oxide) contained in a flue gas to perform denitrification treatment, a desulfurization process of bringing SOx contained in the flue gas in contact with calcium carbonate in slurry to perform desulfurization treatment, and a CO2 desorption process of bringing the flue gas subjected to the denitrification treatment and the desulfurization Docket No. PMHA-16014-PCT
treatment in countercurrent contact with an amine-based absorbent (alkanolamine aqueous solution) in an absorber to cause the absorbent to absorb CO2 in the flue gas, and an absorbent regenerating process of obtaining a lean solution by removing CO2 from a rich solution that has absorbed 002 in a regenerator and returning the lean solution to the absorber again. Then, in this method, to prevent a situation where a thermally stable salt resulted from oxidative degradation of alkanolamine by oxygen in the flue gas or a reaction of alkanolamine with residual NOx or residual S0x, and a solid such as dust contained in the flue gas are accumulated in a system that the absorbent passes through, reclaiming is performed, which includes heating the absorbent in a reclaimer, concentrating a coexisting substance as sludge, and removing the deteriorated substance from the absorbent.
Citation List Patent Literature
treatment in countercurrent contact with an amine-based absorbent (alkanolamine aqueous solution) in an absorber to cause the absorbent to absorb CO2 in the flue gas, and an absorbent regenerating process of obtaining a lean solution by removing CO2 from a rich solution that has absorbed 002 in a regenerator and returning the lean solution to the absorber again. Then, in this method, to prevent a situation where a thermally stable salt resulted from oxidative degradation of alkanolamine by oxygen in the flue gas or a reaction of alkanolamine with residual NOx or residual S0x, and a solid such as dust contained in the flue gas are accumulated in a system that the absorbent passes through, reclaiming is performed, which includes heating the absorbent in a reclaimer, concentrating a coexisting substance as sludge, and removing the deteriorated substance from the absorbent.
Citation List Patent Literature
[0004] Patent Literature 1: Japanese Laid-open Patent Publication No. 5-245339 Summary Technical Problem
[0005] However, in a conventional reclaiming operation, while ionic substances and solid substances having no vapor pressure, and high-boiling point substances are separated and removed as reclaimer residues, low-boiling point substances and substances having a vapor pressure similarly to absorption agents are entrained in recovered vapor recovered from the reclaimer. Therefore, there is a problem that separation/removal of absorbent coexisting component is insufficient.
[0006] Therefore, a reclaiming device that prevents the introduction of an absorbent coexisting component together Docket No. PMHA-16014-PCT
with recovered vapor recovered from a reclaimer to a regenerator, when regenerating an absorbent in the reclaimer, has been desired.
with recovered vapor recovered from a reclaimer to a regenerator, when regenerating an absorbent in the reclaimer, has been desired.
[0007] In view of the foregoing, an objective of the present invention is to provide a reclaiming device, a method, and a recovery unit of CO2, H2S, or both of them, which can prevent entrainment of a fluid in a reclaimer with recovered vapor recovered from a reclaimer, and the introduction of an absorbent coexisting component together with the recovered vapor to the renegerator.
Solution to Problem
Solution to Problem
[0008] The first aspect of the present invention in order to solve the above mentioned problem is a reclaiming device including a reclaimer configured to introduce and store a part of an absorbent regenerated in a regenerator of a recovery unit that recovers CO2 or H25 in a gas, a first alkaline agent supply section configured to supply an alkaline agent to the reclaimer, a heating section configured to heat the absorbent stored in the reclaimer and to which the alkaline agent has been mixed to obtain recovered vapor, a vapor cooler configured to cool the recovered vapor discharged from the reclaimer through a vapor line, a first gas-liquid separator configured to separate a coexisting substance entrained in the cooled recovered vapor into recovered absorption agent vapor and a liquid coexisting substance by gas-liquid separation, and an introduction line configured to introduce the recovered absorption agent vapor separated in the first gas-liquid separator to the regenerator.
[0009] The second aspect of the invention is the reclaiming device according to the first aspect, wherein the first vapor cooler includes a first cooler configured to perform cooling with reflux water from the regenerator, Docket No. PMHA-16014-PCT
and a second cooler provided at a downstream side of a rich/lean solution heat exchanger disposed in a lean solution supply line, and configured to cool the recovered vapor with a rich solution.
and a second cooler provided at a downstream side of a rich/lean solution heat exchanger disposed in a lean solution supply line, and configured to cool the recovered vapor with a rich solution.
[0010] The third aspect of the invention is a reclaiming device including a reclaimer configured to introduce and store a part of an absorbent regenerated in an regenerator of a recovery unit that recovers CO2 or I-12S in a gas, a first alkaline agent supply section configured to supply an alkaline agent to the reclaimer, a heating section configured to heat the absorbent stored in the reclaimer and to which the alkaline agent has been mixed to obtain recovered vapor, a second vapor cooler configured to cool the recovered vapor discharged from the reclaimer through a vapor line, a first gas-liquid separator configured to separate a coexisting substance entrained in the cooled recovered vapor into recovered absorption agent vapor and a liquid coexisting substance by gas-liquid separation, a cooler configured to cool the separated recovered absorption agent vapor, a second gas-liquid separator configured to separate the recovered absorption agent vapor after cooling into a low-boiling point substance flue gas and a recovered absorbent by gas-liquid separation, a heat exchanger configured to perform heat exchange of the liquid coexisting substance separated in the first gas-liquid separator with vapor condensed water from vapor supplied to the reclaimer to increase a temperature, a CO2 absorber configured to bring the liquid coexisting substance after increase in the temperature and a CO2 gas in contact, a second alkaline agent supply section configured to supply the alkaline agent to the liquid coexisting substance after absorption of CO2, and a distiller configured to distill the liquid coexisting substance to which the alkaline agent Docket No. PMHA-16014-PCT
has been supplied while introducing the 002 thereinto.
has been supplied while introducing the 002 thereinto.
[0011] The fourth aspect of the invention is the reclaiming device according to the third aspect, wherein the second vapor cooler includes a first cooler configured 5 to perform cooling with the liquid coexisting substance separated from the recovered vapor in the first gas-liquid separator by gas-liquid separation, a second cooler configured to perform cooling with reflux water from the regenerator, and a third cooler provided at a downstream side of a rich/lean solution heat exchanger disposed in a lean solution supply line, and configured to cool, with a rich solution, the recovered vapor after cooling with the second cooler.
[0012] The fifth aspect of the invention is the reclaiming device according to the third or fourth aspect, including a 002 gas introduction line configured to introduce the 002 discharged from the 002 absorber into the distiller, and a nitrogen supply section configured to introduce a nitrogen gas into the 002 gas introduction line.
[0013] The sixth aspect of the invention is a reclaiming method including, when recovering, in a reclaimer, a part of circulating absorbent that recovers 002 or H2S in a flue gas in a 002 or H2S recovery unit as recovered vapor, cooling the recovered vapor from the reclaimer, and then separating an entrained coexisting substance by gas-liquid separation to remove a liquid coexisting substance, and introducing recovered absorption agent vapor after the gas-liquid separation into an absorbent regenerator.
[0014] The seventh aspect of the invention is the reclaiming method according to the sixth aspect, including cooling the recovered absorption agent vapor to obtain a liquid recovered absorbent in the introducing the recovered absorption agent vapor after separation into the absorbent Docket No. PMHA-16014-PCT
regenerator, heating the separated liquid coexisting substance, then bringing the liquid coexisting substance and a CO2 gas in contact, and then supplying an alkaline agent, and distilling, in a distiller, the liquid coexisting substance into which the alkaline agent has been supplied while introducing the CO2 thereto.
regenerator, heating the separated liquid coexisting substance, then bringing the liquid coexisting substance and a CO2 gas in contact, and then supplying an alkaline agent, and distilling, in a distiller, the liquid coexisting substance into which the alkaline agent has been supplied while introducing the CO2 thereto.
[0015] The eighth aspect of the invention is the reclaiming method according to the seventh aspect, wherein a nitrogen gas is added to the CO2 gas to be introduced into the distiller.
[0016] The ninth aspect of the invention is a recovery unit of CO2, H2S, or both of CO2 and H2S, including an absorber configured to bring a gas containing CO2, H2S, or both of CO2 and H2S and an absorbent in contact to remove CO2, H2S, or both of CO2 and H2S, an absorbent regenerator configured to regenerate a solution that has absorbed CO2, H2S, or both of CO2 and H2S to obtain the absorbent, and the reclaiming device according to any one of the first to the fifth aspects, configured to extract a part of the absorbent regenerated in the regenerator, and to remove a coexisting substance in the absorbent, wherein the absorbent regenerated in the absorbent regenerator is circulated and reused in the absorber, and recovered vapor recovered from the reclaiming device is introduced into the regenerator.
Advantageous Effects of Invention
Advantageous Effects of Invention
[0017] According to the present invention, by performing selective separation/removal of an absorbent coexisting component entrained in recovered vapor from a reclaimer, improvement of operation reliability including reduction of absorbent corrosiveness can be achieved. Further, improvement of absorption agent recovery performance can be achieved.
Docket No. PMHA-16014-PCT
Brief Description of Drawings
Docket No. PMHA-16014-PCT
Brief Description of Drawings
[0018] FIG. 1 is a schematic diagram of a CO2 recovery unit according to a first embodiment.
FIG. 2 is a schematic diagram of a reclaiming device according to the first embodiment.
FIG. 3 is a schematic diagram of another reclaiming device according to the first embodiment.
FIG. 4 is a schematic diagram of a reclaiming device according to a second embodiment.
FIG. 5 is a schematic diagram of another reclaiming device according to the second embodiment.
FIG. 6 is a schematic diagram of a reclaiming device according to a third embodiment.
FIG. 7 is a diagram illustrating selective removal ratios in recovered vapor in a conventional example and the first embodiment.
FIG. 8 is a diagram illustrating selective removal ratios in recovered vapor in a conventional example and the second embodiment.
FIG. 9 is a diagram illustrating recovery ratios of an absorption agent in the first embodiment and the second embodiment.
FIG. 10 is a diagram illustrating selective removal ratios in recovered vapor in a conventional example and the third embodiment.
FIG. 11 is a diagram illustrating recovery ratios of an absorption agent in the first embodiment and the third embodiment.
Description of Embodiments
FIG. 2 is a schematic diagram of a reclaiming device according to the first embodiment.
FIG. 3 is a schematic diagram of another reclaiming device according to the first embodiment.
FIG. 4 is a schematic diagram of a reclaiming device according to a second embodiment.
FIG. 5 is a schematic diagram of another reclaiming device according to the second embodiment.
FIG. 6 is a schematic diagram of a reclaiming device according to a third embodiment.
FIG. 7 is a diagram illustrating selective removal ratios in recovered vapor in a conventional example and the first embodiment.
FIG. 8 is a diagram illustrating selective removal ratios in recovered vapor in a conventional example and the second embodiment.
FIG. 9 is a diagram illustrating recovery ratios of an absorption agent in the first embodiment and the second embodiment.
FIG. 10 is a diagram illustrating selective removal ratios in recovered vapor in a conventional example and the third embodiment.
FIG. 11 is a diagram illustrating recovery ratios of an absorption agent in the first embodiment and the third embodiment.
Description of Embodiments
[0019] Hereinafter, favorable embodiments of the present invention will be described in detail with reference to the appended drawings. Note that the present invention is not limited by the embodiments, and when there is a plurality Docket No. PMHA-16014-PCT
of embodiments, the present invention includes those obtained by combining the embodiments.
[First Embodiment]
of embodiments, the present invention includes those obtained by combining the embodiments.
[First Embodiment]
[0020] While an employable process to remove 002, H2S, or both of them in a gas of the present invention is not especially limited, an example of a removing device that removes 002 will be described with reference to FIG. 1.
[0021] Examples of gases to be treated by the present invention include a coal gasifier gas, a synthesis gas, a coke oven gas, a petroleum gas, a natural gas, and a combustion flue gas. However, the gases are not limited to these examples, and any gas can be employed as long as the gas contains an acid gas such as 002 or H2S.
In the following embodiment, a flue gas containing CO2 as the acid gas will be described.
In the following embodiment, a flue gas containing CO2 as the acid gas will be described.
[0022] FIG. 1 is a schematic diagram illustrating a configuration of a 002 recovery unit according to the first embodiment. As illustrated in FIG. 1, a 002 recovery unit 12 according to the first embodiment includes a flue gas cooling device 16 that cools a flue gas 14 containing 002 and 02 discharged from an industrial combustion facility 13 such as a boiler or a gas turbine with cooling water 15, a 002 absorber (hereinafter, also referred to as "absorber") 18 including a 002 recovery section 18A that brings the cooled flue gas 14 containing 002 and a 002 absorbent (hereinafter, also referred to as "absorbent") 17 that absorbs 002 in contact to remove 002 from the flue gas 14, and an absorbent regenerator (hereinafter, also referred to as "regenerator") 20 that desorbs 002 from a 002 absorbent (hereinafter, also referred to as "rich solution") 19 that has absorbed 002 to regenerate a 002 absorbent. Then, in the 002 recovery unit 12, the regenerated 002 absorbent (hereinafter, also referred to as "lean solution") 17 from DocketNo.PMHA-104-10CT
which CO2 has been removed in the absorbent regenerator 20 is reused in the CO2 absorber 18 as the CO2 absorbent.
which CO2 has been removed in the absorbent regenerator 20 is reused in the CO2 absorber 18 as the CO2 absorbent.
[0023] Note that, in FIG. 1, the reference sign 13a is a flue gas duct, 13b is a stack, 27a is steam condensed water.
There are two cases for the CO2 recovery unit 12, which includes a case of providing the CO2 recovery unit later to recover CO2 from an already provided flue gas source, and a case of placing the CO2 recovery unit along with a newly provided flue gas source at the same time. An openable/closable damper is installed to the stack 13b, and is closed at the time of an operation of the CO2 recovery unit 12. Further, the damper is set to open when the operation of the CO2 recovery unit 12 is stopped although the flue gas source is operated.
There are two cases for the CO2 recovery unit 12, which includes a case of providing the CO2 recovery unit later to recover CO2 from an already provided flue gas source, and a case of placing the CO2 recovery unit along with a newly provided flue gas source at the same time. An openable/closable damper is installed to the stack 13b, and is closed at the time of an operation of the CO2 recovery unit 12. Further, the damper is set to open when the operation of the CO2 recovery unit 12 is stopped although the flue gas source is operated.
[0024] In a method of recovering CO2 using the CO2 recovery unit 12, first, a pressure of the flue gas 14 containing CO2 from the industrial combustion facility 13 such as a boiler or a gas turbine is increased by a flue gas blower 22, and the flue gas 14 is then sent to the flue gas cooling device 16, cooled with the cooling water 15, and sent to the CO2 absorber 18.
[0025] In the CO2 absorber 18, the flue gas 14 is brought in countercurrent contact with the CO2 absorbent 17 that is an amine absorbent according to the present embodiment, and CO2 in the flue gas 14 is absorbed in the CO2 absorbent 17 by a chemical reaction.
The 002-removed flue gas from which CO2 has been removed in the CO2 recovery section 18A is brought in gas-liquid contact with circulating rinse water 21 containing the CO2 absorbent supplied through a nozzle in a water cleaning section 18B of the CO2 absorber 18, the CO2 absorbent 17 entrained in the 002-removed flue gas is recovered, and then a flue gas 23 from which CO2 has been Docket No. PMHA-16014-PCT
removed is discharged outside the system.
Further, a pressure of the rich solution that is the 002-absorbed 002 absorbent 19 is increased by a rich solution pump 24, heated with the lean solution that is the 5 002 absorbent 17 regenerated in the absorbent regenerator 20, in a rich/lean solution heat exchanger 25 disposed on a rich solution supply line 1,1, and supplied to the absorbent regenerator 20.
The 002-removed flue gas from which CO2 has been removed in the CO2 recovery section 18A is brought in gas-liquid contact with circulating rinse water 21 containing the CO2 absorbent supplied through a nozzle in a water cleaning section 18B of the CO2 absorber 18, the CO2 absorbent 17 entrained in the 002-removed flue gas is recovered, and then a flue gas 23 from which CO2 has been Docket No. PMHA-16014-PCT
removed is discharged outside the system.
Further, a pressure of the rich solution that is the 002-absorbed 002 absorbent 19 is increased by a rich solution pump 24, heated with the lean solution that is the 5 002 absorbent 17 regenerated in the absorbent regenerator 20, in a rich/lean solution heat exchanger 25 disposed on a rich solution supply line 1,1, and supplied to the absorbent regenerator 20.
[0026] The rich solution 19 discharged from an upper 10 portion to an inside of the absorbent regenerator 20 causes an endothermic reaction by water vapor supplied from a bottom portion, and desorbs most of 002. The CO2 absorbent that has desorbed a part or most of CO2 in the absorbent regenerator 20 is called semi-lean solution. This semi-lean solution becomes the CO2 absorbent (lean solution) 17 from which nearly all of CO2 has been removed, when the semi-lean solution is about to reach the bottom portion of the absorbent regenerator 20. A part of the lean solution 17 is heated with water vapor 27 in a regenerating heater 26, and supplies water vapor to the inside of the absorbent regenerator 20.
[0027] Meanwhile, a 002-entrained gas 28 accompanied by the water vapor discharged from the rich solution 19 and the semi-lean solution in the regenerator is led from a top of the absorbent regenerator 20, the water vapor is condensed by a condenser 29, water is separated in a separation drum 30, and a CO2 gas 40 is discharged outside the system and is separately compressed by a compressor 41 and recovered. This compressed/recovered 002 gas 42 is pressed into an oil field using an enhanced oil recovery method (EOR) or stored in an aquifer after through a separation drum 43 to achieve measurements against the global warming.
Docket No. PMHA-16014-PCT
Reflux water 31 separated/refluxed from the CO2 entrained gas 28 accompanied by the water vapor in the separation drum 30 is supplied to the upper portion of the absorbent regenerator 20 and the rinse water 21 side with a reflux water circulation pump 35.
Docket No. PMHA-16014-PCT
Reflux water 31 separated/refluxed from the CO2 entrained gas 28 accompanied by the water vapor in the separation drum 30 is supplied to the upper portion of the absorbent regenerator 20 and the rinse water 21 side with a reflux water circulation pump 35.
[0028] The regenerated CO2 absorbent (lean solution) 17 is cooled with the rich solution 19 in the rich/lean solution heat exchanger 25 disposed on an intersection of the rich solution supply line L1 and a lean solution supply line L2, then a pressure is increased by a lean solution pump 32, and the CO2 absorbent (lean solution) 17 is cooled in a lean solution cooler 33 and is then supplied to the CO2 absorber 18. Note that, in this embodiment, an outline has been merely described. Description is given omitting a part of devices that come with the CO2 recovery unit.
[0029] A part of the CO2 absorbent 17 regenerated in the absorbent regenerator 20 is branched at a branch line L11 from the lean solution supply line L2 and introduced into a reclaimer 51, and the water vapor 27 is supplied to indirectly heat the absorbent, so that a coexisting substance is separated.
[0030] FIG. 2 is a schematic diagram of a reclaiming device according to the first embodiment.
As illustrated in FIG. 2, a reclaiming device according to the present embodiment includes the reclaimer 51 that introduces, through a branch line Lll, and stores a part 17a of the absorbent 17 regenerated in the regenerator of the recovery unit that recovers CO2 or H2S in a gas, a first alkaline agent supply section 53A that supplies an alkaline agent 52 to the reclaimer 51, a heating section 54 that heats the absorbent 17 stored in the reclaimer 51 and to which the alkaline agent 52 has been mixed to obtain recovered vapor 61, a first vapor cooler 55A that cools the Docket No. PMHA-16014-PCT
recovered vapor 61 discharged from the reclaimer 51 through a vapor line L12, a first gas-liquid separator 56A that separates a coexisting substance 62 entrained in the cooled recovered vapor 61 into recovered absorption agent vapor (gas) 17b and a liquid coexisting substance 62 by gas-liquid separation, and an introduction line L13 that introduces the recovered absorption agent vapor 17b separated in the first gas-liquid separator 56A into the regenerator 20.
Note that the reference sign 57 in the drawing illustrates a coexisting substance cooler that cools the coexisting substance (liquid) 62 after the gas-liquid separation, and the reference sign 58 illustrates a reclaimer residue.
As illustrated in FIG. 2, a reclaiming device according to the present embodiment includes the reclaimer 51 that introduces, through a branch line Lll, and stores a part 17a of the absorbent 17 regenerated in the regenerator of the recovery unit that recovers CO2 or H2S in a gas, a first alkaline agent supply section 53A that supplies an alkaline agent 52 to the reclaimer 51, a heating section 54 that heats the absorbent 17 stored in the reclaimer 51 and to which the alkaline agent 52 has been mixed to obtain recovered vapor 61, a first vapor cooler 55A that cools the Docket No. PMHA-16014-PCT
recovered vapor 61 discharged from the reclaimer 51 through a vapor line L12, a first gas-liquid separator 56A that separates a coexisting substance 62 entrained in the cooled recovered vapor 61 into recovered absorption agent vapor (gas) 17b and a liquid coexisting substance 62 by gas-liquid separation, and an introduction line L13 that introduces the recovered absorption agent vapor 17b separated in the first gas-liquid separator 56A into the regenerator 20.
Note that the reference sign 57 in the drawing illustrates a coexisting substance cooler that cools the coexisting substance (liquid) 62 after the gas-liquid separation, and the reference sign 58 illustrates a reclaimer residue.
[0031] The temperature of the recovered vapor 61 discharged from the reclaimer 51 is decreased by the first vapor cooler 55A by about 6 to 7 C.
[0032] In the reclaimer 51, the coexisting substance 62 having a vapor pressure is entrained in the recovered vapor 61. Therefore, the entrained coexisting substance 62 can be separated and removed by performing separation using the first gas-liquid separator 56A as in the present embodiment.
[0033] That is, the coexisting substance 62 having a higher boiling point than amines in a free state of the absorbent is cooled in the first vapor cooler 55A, and the temperature is decreased by about 6 to 7 C, so that the coexisting substance 62 is liquefied and separated in the first gas-liquid separator 56A. When a temperature (T1) of the recovered vapor 61 is 130 C, the recovered vapor 61 is cooled in the first vapor cooler 55A, and a temperature (T2) of the recovered vapor 61 after cooling is made to 123 C, so that the coexisting substance (liquid) 62 can be separated.
Docket No. PMHA-16014-PCT
Docket No. PMHA-16014-PCT
[0034] An effect of the present embodiment will be described with reference to FIG. 7.
FIG. 7 is a diagram illustrating selective removal ratios in recovered vapor in a conventional example and the first embodiment (where the conventional example is a reference (1)). The conventional technology is a case of recovering the recovered vapor 61 from the reclaimer 51 as it is without providing the gas-liquid separator as in the present embodiment.
The selection removal ratio of the coexisting substance 62 from the recovered vapor 61 in the present embodiment is 40, and the coexisting substance can be substantially removed, where the conventional example is the reference (1).
FIG. 7 is a diagram illustrating selective removal ratios in recovered vapor in a conventional example and the first embodiment (where the conventional example is a reference (1)). The conventional technology is a case of recovering the recovered vapor 61 from the reclaimer 51 as it is without providing the gas-liquid separator as in the present embodiment.
The selection removal ratio of the coexisting substance 62 from the recovered vapor 61 in the present embodiment is 40, and the coexisting substance can be substantially removed, where the conventional example is the reference (1).
[0035] Further, in the present embodiment, as illustrated in FIG. 3, a first cooler 55A-1 that performs cooling using the reflux water 31 from the regenerator 20 of the CO2 recovery unit 12, and a second cooler 55A-2 provided at a downstream side of a rich/lean solution heat exchanger 25 disposed at an intersection of the rich solution supply line L1 and the lean solution supply line L2, and which cools the recovered vapor 61 with the rich solution 19 are included as the first vapor cooler 55A.
[0036] Accordingly, when the temperature (Ti) of the recovered vapor 61 is 130 C, the recovered vapor is cooled to the temperature (T2 = 125 C) by the first cooler 55A-1, and then cooled to a temperature (T3 = 123 C) by the second cooler 55A-2.
Here, the reflux water 31 is brought to pass through a coexisting substance cooler 57 for cooling the coexisting substance (liquid) 62 separated in the first gas-liquid separator 56A, and is then introduced into the first cooler 55A-1 through a cooling water line L14.
Docket No. PMHA-16014-PCT
The first cooler 55A-1 is provided at an intersection of the vapor line L12 and the cooling water line L14 and the second cooler 55A-2 is provided at an intersection of the vapor line L12 and the rich solution supply line Ll, and thus cooling is possible with heat in the system of the 002 recovery unit 12.
[Second Embodiment]
Here, the reflux water 31 is brought to pass through a coexisting substance cooler 57 for cooling the coexisting substance (liquid) 62 separated in the first gas-liquid separator 56A, and is then introduced into the first cooler 55A-1 through a cooling water line L14.
Docket No. PMHA-16014-PCT
The first cooler 55A-1 is provided at an intersection of the vapor line L12 and the cooling water line L14 and the second cooler 55A-2 is provided at an intersection of the vapor line L12 and the rich solution supply line Ll, and thus cooling is possible with heat in the system of the 002 recovery unit 12.
[Second Embodiment]
[0037] A reclaiming device according to an embodiment of the present invention will be described with reference to the drawings. FIG. 4 is a schematic diagram of a reclaiming device according to a second embodiment. FIG. 5 is a schematic diagram of another reclaiming device according to the second embodiment. Note that the same member as the first embodiment is denoted with the same reference sign, and description thereof is omitted.
As illustrated in FIG. 4, a reclaiming device according to the present embodiment includes a reclaimer 51 that introduces, through a branch line Lll, and stores a part 17a of an absorbent 17 regenerated in a regenerator of a recovery unit that recovers 002 or H2S in a gas, a first alkaline agent supply section 53A that supplies an alkaline agent 52 to the reclaimer 51, a heating section 54 that heats the absorbent 17 stored in the reclaimer 51 and to which the alkaline agent 52 has been mixed to obtain recovered vapor 61, a second vapor cooler 55B that cools recovered vapor 61 discharged from the reclaimer 51 through a vapor line L12, a first gas-liquid separator 56A that separates a coexisting substance 62 entrained in the cooled recovered vapor 61 into recovered absorption agent vapor (gas) 17b and a liquid coexisting substance 62 by gas-liquid separation, a fourth cooler 71 that cools the separated recovered absorption agent vapor 17b, a second gas-liquid separator 563 that separates the recovered Docket No. PMHA-16014-PCT
absorption agent vapor 17b after cooling into a low-boiling point substance flue gas 72 and a recovered absorbent 17c by gas-liquid separation, a heat exchanger 63 that performs heat exchange of the liquid coexisting substance 62 5 separated in the first gas-liquid separator 56A with vapor condensed water 27a from vapor 27 supplied to the reclaimer 51 to increase the temperature, a CO2 absorber 64 that brings the liquid coexisting substance 62 after increase in the temperature, and a CO2 gas (recovered 002) 40 in 10 contact, a second alkaline agent supply section 53B that supplies an alkaline agent 52 to a liquid coexisting substance 62A after absorption of 002, and a distiller 68 that distills a liquid coexisting substance 62B to which the alkaline agent 52 has been supplied while introducing 15 the CO2 gas (recovered 002) 40 thereto. Further, a coexisting substance (liquid) 63A is discharged from the distiller 68. Further, CO2 discharged from the CO2 absorber 64 is introduced into the distiller 68 through a CO2 gas introduction line L21-
As illustrated in FIG. 4, a reclaiming device according to the present embodiment includes a reclaimer 51 that introduces, through a branch line Lll, and stores a part 17a of an absorbent 17 regenerated in a regenerator of a recovery unit that recovers 002 or H2S in a gas, a first alkaline agent supply section 53A that supplies an alkaline agent 52 to the reclaimer 51, a heating section 54 that heats the absorbent 17 stored in the reclaimer 51 and to which the alkaline agent 52 has been mixed to obtain recovered vapor 61, a second vapor cooler 55B that cools recovered vapor 61 discharged from the reclaimer 51 through a vapor line L12, a first gas-liquid separator 56A that separates a coexisting substance 62 entrained in the cooled recovered vapor 61 into recovered absorption agent vapor (gas) 17b and a liquid coexisting substance 62 by gas-liquid separation, a fourth cooler 71 that cools the separated recovered absorption agent vapor 17b, a second gas-liquid separator 563 that separates the recovered Docket No. PMHA-16014-PCT
absorption agent vapor 17b after cooling into a low-boiling point substance flue gas 72 and a recovered absorbent 17c by gas-liquid separation, a heat exchanger 63 that performs heat exchange of the liquid coexisting substance 62 5 separated in the first gas-liquid separator 56A with vapor condensed water 27a from vapor 27 supplied to the reclaimer 51 to increase the temperature, a CO2 absorber 64 that brings the liquid coexisting substance 62 after increase in the temperature, and a CO2 gas (recovered 002) 40 in 10 contact, a second alkaline agent supply section 53B that supplies an alkaline agent 52 to a liquid coexisting substance 62A after absorption of 002, and a distiller 68 that distills a liquid coexisting substance 62B to which the alkaline agent 52 has been supplied while introducing 15 the CO2 gas (recovered 002) 40 thereto. Further, a coexisting substance (liquid) 63A is discharged from the distiller 68. Further, CO2 discharged from the CO2 absorber 64 is introduced into the distiller 68 through a CO2 gas introduction line L21-
[0038] In the present embodiment, the recovered vapor 61 is cooled in the second vapor cooler 55B, and then separated into recovered absorption agent vapor (gas) 17b and the liquid coexisting substance 62 by gas-liquid separation in the first gas-liquid separator 56A.
A volatile low-boiling point substance such as ammonia is entrained in this recovered adsorbent vapor (gas) 17b.
Therefore, the recovered adsorbent vapor (gas) 17 is cooled in a fourth cooler 71 and is introduced into the second gas-liquid separator 563, and the low-boiling point substance flue gas 72 is separated. This separated low-boiling point substance flue gas 72 is introduced into a top of the absorber 18. Reflux water 31 from a CO2 recovery unit 12 is introduced into the fourth cooler 71 to Docket No. PMHA-16014-PCT
perform cooling.
A volatile low-boiling point substance such as ammonia is entrained in this recovered adsorbent vapor (gas) 17b.
Therefore, the recovered adsorbent vapor (gas) 17 is cooled in a fourth cooler 71 and is introduced into the second gas-liquid separator 563, and the low-boiling point substance flue gas 72 is separated. This separated low-boiling point substance flue gas 72 is introduced into a top of the absorber 18. Reflux water 31 from a CO2 recovery unit 12 is introduced into the fourth cooler 71 to Docket No. PMHA-16014-PCT
perform cooling.
[0039] Further, the temperature of the separated liquid coexisting substance 62 is increased in the heat exchanger 63 by subjecting to heat exchange with the vapor condensed water 27a from the vapor 27 supplied to the reclaimer 51, and the liquid coexisting substance 62 after increase in the temperature is introduced into the 002 absorber 64 into which a 002 gas 40 is introduced. In the 002 absorber 64, the liquid coexisting substance 62 is brought into countercurrent contact with the recovered 002 gas 40 to react with 002. As the 002 gas 40, the 002 gas 40 recovered in the 002 recovery unit 12 is used.
[0040] Following that, amines of the absorption agent are made into amines in a free state by supplying the alkaline agent 52 from the second alkaline agent supply section 53B to the liquid coexisting substance 62A, and making a pH of the liquid coexisting substance 62A high (for example, by about 0.3 to 0.5).
Following that, the liquid coexisting substance 623 to which the alkaline agent 52 has been added is introduced into the distiller 68, and in performing distillation here, the coexisting substance 62B absorbs the introduced 002 gas 40 and is on a liquid side. Therefore, the coexisting substance 62B loses a vapor pressure.
The absorption agent is in a vapor state with a high pH by release of a release valve 67. Therefore, the absorption agent does not react with the 002 gas 40 and is separated as vapor by the distillation in the distiller 68.
Following that, the liquid coexisting substance 623 to which the alkaline agent 52 has been added is introduced into the distiller 68, and in performing distillation here, the coexisting substance 62B absorbs the introduced 002 gas 40 and is on a liquid side. Therefore, the coexisting substance 62B loses a vapor pressure.
The absorption agent is in a vapor state with a high pH by release of a release valve 67. Therefore, the absorption agent does not react with the 002 gas 40 and is separated as vapor by the distillation in the distiller 68.
[0041] Here, the 002 gas 40 introduced into the distiller 68 is 002 discharged from the 002 absorber 64 and introduced through the 002 gas introduction line L21.
The coexisting substance (liquid) 63A separated in the distiller 68 is cooled in a coexisting substance cooler 57.
Docket No. PMHA-16014-PCT
Note that, as a refrigerant used in the coexisting substance cooler 57, the reflux water 31 from the 002 recovery unit 12 is introduced to perform cooling in the present embodiment. Then, the cooled reflux water 31 is introduced into the fourth cooler 71 through a cooling water line L14, and then introduced into the reclaimer 51.
The coexisting substance (liquid) 63A separated in the distiller 68 is cooled in a coexisting substance cooler 57.
Docket No. PMHA-16014-PCT
Note that, as a refrigerant used in the coexisting substance cooler 57, the reflux water 31 from the 002 recovery unit 12 is introduced to perform cooling in the present embodiment. Then, the cooled reflux water 31 is introduced into the fourth cooler 71 through a cooling water line L14, and then introduced into the reclaimer 51.
[0042] An effect of the present embodiment will be described with reference to FIG. 8.
FIG. 8 is a diagram illustrating selective removal ratios in recovered vapor in a conventional example and the second embodiment (where the conventional example is a reference (1)). The conventional technology is a case of recovering the recovered vapor 61 from the reclaimer 51 as it is without providing the first gas-liquid separator 56A
and the second gas-liquid separator 56B as in the present embodiment.
The selection removal ratio of the coexisting substance 62 from the recovered vapor 61 in the present embodiment is 30, and the coexisting substance can be substantially removed, where the conventional example is the reference (1).
FIG. 8 is a diagram illustrating selective removal ratios in recovered vapor in a conventional example and the second embodiment (where the conventional example is a reference (1)). The conventional technology is a case of recovering the recovered vapor 61 from the reclaimer 51 as it is without providing the first gas-liquid separator 56A
and the second gas-liquid separator 56B as in the present embodiment.
The selection removal ratio of the coexisting substance 62 from the recovered vapor 61 in the present embodiment is 30, and the coexisting substance can be substantially removed, where the conventional example is the reference (1).
[0043] FIG. 9 is a diagram illustrating recovery ratios of the absorption agent in the first embodiment and the second embodiment (where the first embodiment is a reference (1)).
In a case of providing the first gas-liquid separator 56A, the second gas-liquid separator 56B, the 002 absorber 64, and the distiller 68 as in the second embodiment, the recovery of the absorption agent from the recovered vapor 61 is improved by about 1.3 times.
In a case of providing the first gas-liquid separator 56A, the second gas-liquid separator 56B, the 002 absorber 64, and the distiller 68 as in the second embodiment, the recovery of the absorption agent from the recovered vapor 61 is improved by about 1.3 times.
[0044] Next, another reclaiming device according to the second embodiment will be described.
FIG. 5 is a schematic diagram of another reclaiming Docket No, PMHA-16014-PCT
device according to the second embodiment.
In the present embodiment, as illustrated in FIG. 5, a first cooler 55B-1 that performs cooling with the coexisting substance 62 separated from the recovered vapor 61 in the first gas-liquid separator 56A, a second cooler 55B-2 that performs cooling using the reflux water 31 from a regenerator 20 of the CO2 recovery unit 12, and a third cooler 55B-3 provided at a downstream side of a rich/lean solution heat exchanger 25 disposed in a lean solution supply line Ll, and which cools the recovered vapor 61 with a rich solution 19 are included as the second vapor cooler 55B.
FIG. 5 is a schematic diagram of another reclaiming Docket No, PMHA-16014-PCT
device according to the second embodiment.
In the present embodiment, as illustrated in FIG. 5, a first cooler 55B-1 that performs cooling with the coexisting substance 62 separated from the recovered vapor 61 in the first gas-liquid separator 56A, a second cooler 55B-2 that performs cooling using the reflux water 31 from a regenerator 20 of the CO2 recovery unit 12, and a third cooler 55B-3 provided at a downstream side of a rich/lean solution heat exchanger 25 disposed in a lean solution supply line Ll, and which cools the recovered vapor 61 with a rich solution 19 are included as the second vapor cooler 55B.
[0045] Accordingly, when a temperature (T1) of the recovered vapor 61 is 130 C, the recovered vapor is cooled to a temperature (T2 = 128 C) by the first cooler 55B-1, then cooled to a temperature (T3 = 125 C) by the second cooler 55B-2, and then cooled to a temperature (T4 - 123 C) by the third cooler 55B-3.
Here, after the reflux water 31 performs cooling in the fourth cooler 71 for cooling that cools the recovered absorption agent vapor (gas) 17b separated in the first gas-liquid separator 56A, the reflux water 31 is introduced into the second cooler 55B-2 through the cooling water line L14, and further performs cooling.
Note that the first cooler 55B-1 is provided at an intersection of the vapor line L12 and a liquid coexisting substance discharge line L16, the second cooler 55B-2 is provided at an intersection of the vapor line L12 and the cooling water line L14, and the third cooler 55B-3 is provided at an intersection of the vapor line L12 and a rich solution line Ll, and thus cooling is possible with heat in the system of the CO2 recovery unit 12.
[Third Embodiment]
Docket No, PMHA-16014-PCT
Here, after the reflux water 31 performs cooling in the fourth cooler 71 for cooling that cools the recovered absorption agent vapor (gas) 17b separated in the first gas-liquid separator 56A, the reflux water 31 is introduced into the second cooler 55B-2 through the cooling water line L14, and further performs cooling.
Note that the first cooler 55B-1 is provided at an intersection of the vapor line L12 and a liquid coexisting substance discharge line L16, the second cooler 55B-2 is provided at an intersection of the vapor line L12 and the cooling water line L14, and the third cooler 55B-3 is provided at an intersection of the vapor line L12 and a rich solution line Ll, and thus cooling is possible with heat in the system of the CO2 recovery unit 12.
[Third Embodiment]
Docket No, PMHA-16014-PCT
[0046] A reclaiming device according to an embodiment of the present invention will be described with reference to the drawing. FIG. 6 is a schematic diagram of a reclaiming device according to a third embodiment. Note that the same member as the first and second embodiments is denoted with the same reference sign, and description thereof is omitted.
As illustrated in FIG. 6, the reclaiming device according to the present embodiment further includes a CO2 gas introduction line L21 through which a CO2 gas 40 discharged from a CO2 absorber 64 is introduced into a distiller 68, and a nitrogen supply section 69 that introduces a nitrogen (N2) gas into the CO2 gas introduction line L21, in the reclaiming device of the second embodiment.
As illustrated in FIG. 6, the reclaiming device according to the present embodiment further includes a CO2 gas introduction line L21 through which a CO2 gas 40 discharged from a CO2 absorber 64 is introduced into a distiller 68, and a nitrogen supply section 69 that introduces a nitrogen (N2) gas into the CO2 gas introduction line L21, in the reclaiming device of the second embodiment.
[0047] Since the N2 gas is added to the CO2 gas 40 from the nitrogen supply section 69, a CO2 partial pressure in the distiller 68 can be decreased. In this case, since N2 is mixed in a recovered absorption agent (gas body), it is desirable to supply the N2 gas to a bottom of an absorber 18 in a case of recovering CO2 as a product. When there is no problem with the purity of the CO2 product, the CO2 may be put back to a regenerator 20, as illustrated in FIG. 6.
[0048] An effect of the present embodiment will be described with reference to FIG. 10.
FIG. 10 is a diagram illustrating selective removal ratios in recovered vapor in a conventional example and the third embodiment (where the conventional example is a reference (1)). The conventional technology is a case of recovering the recovered vapor 61 from a reclaimer 51 as it is without providing a first gas-liquid separator 56A, a second gas-liquid separator 56B, a CO2 absorber 64, and the distiller 68 as in the present embodiment.
The selection removal ratio of a coexisting substance Docket No, PMHA-16014-PCT
62 from recovered vapor 61 in the present embodiment is 35, and the coexisting substance can be substantially removed, where the conventional example is the reference (1).
FIG. 10 is a diagram illustrating selective removal ratios in recovered vapor in a conventional example and the third embodiment (where the conventional example is a reference (1)). The conventional technology is a case of recovering the recovered vapor 61 from a reclaimer 51 as it is without providing a first gas-liquid separator 56A, a second gas-liquid separator 56B, a CO2 absorber 64, and the distiller 68 as in the present embodiment.
The selection removal ratio of a coexisting substance Docket No, PMHA-16014-PCT
62 from recovered vapor 61 in the present embodiment is 35, and the coexisting substance can be substantially removed, where the conventional example is the reference (1).
[0049] FIG. 11 is a diagram illustrating recovery ratios 5 of the absorption agent in the first embodiment and the third embodiment (where the first embodiment is the reference (1)).
By introduction of nitrogen as in the third embodiment, the 002 partial pressure is decreased, addition of an 10 alkaline agent 52 can be decreased, and the recovery ratio of the absorption agent from the recovered vapor 61 is improved by about 1.3 times.
Reference Signs List
By introduction of nitrogen as in the third embodiment, the 002 partial pressure is decreased, addition of an 10 alkaline agent 52 can be decreased, and the recovery ratio of the absorption agent from the recovered vapor 61 is improved by about 1.3 times.
Reference Signs List
[0050] 12 002 recovery unit 15 13 Industrial combustion facility 14 Flue gas 16 Flue gas cooling device 17 002 absorbent (lean solution) 18 CO2 absorber 20 19 CO2-absorbed 002 absorbent (rich solution) 20 Absorbent regenerator 21 Rinse water
51 Reclaimer
52 Alkaline agent 55A First vapor cooler 553 Second vapor cooler 56A First gas-liquid separator 56B Second gas-liquid separator 61 Recovered vapor 62 Coexisting substance
Claims (9)
1. A reclaiming device comprising:
a reclaimer configured to introduce and store a part of an absorbent regenerated in an absorbent regenerator of a recovery unit that recovers CO2 or H2S in a gas;
a first alkaline agent supply section configured to supply an alkaline agent to the reclaimer;
a heating section configured to heat the absorbent stored in the reclaimer and to which the alkaline agent has been mixed to obtain recovered vapor;
a first vapor cooler configured to cool the recovered vapor discharged from the reclaimer through a vapor line;
a first gas-liquid separator configured to separate a coexisting substance entrained in the cooled recovered vapor into recovered absorption agent vapor and a liquid coexisting substance by gas-liquid separation; and an introduction line configured to introduce the recovered absorption agent vapor separated in the first gas-liquid separator to the absorbent regenerator.
a reclaimer configured to introduce and store a part of an absorbent regenerated in an absorbent regenerator of a recovery unit that recovers CO2 or H2S in a gas;
a first alkaline agent supply section configured to supply an alkaline agent to the reclaimer;
a heating section configured to heat the absorbent stored in the reclaimer and to which the alkaline agent has been mixed to obtain recovered vapor;
a first vapor cooler configured to cool the recovered vapor discharged from the reclaimer through a vapor line;
a first gas-liquid separator configured to separate a coexisting substance entrained in the cooled recovered vapor into recovered absorption agent vapor and a liquid coexisting substance by gas-liquid separation; and an introduction line configured to introduce the recovered absorption agent vapor separated in the first gas-liquid separator to the absorbent regenerator.
2. The reclaiming device according to claim 1, wherein the first vapor cooler includes a first cooler configured to perform cooling with reflux water from the absorbent regenerator, and a second cooler provided at a downstream side of a rich/lean solution heat exchanger disposed in a lean solution supply line, and configured to cool the recovered vapor with a rich solution.
3. A reclaiming device comprising:
a reclaimer configured to introduce and store a part of an absorbent regenerated in an absorbent regenerator of a recovery unit that recovers CO2 or H2S in a gas;
a first alkaline agent supply section configured to supply an alkaline agent to the reclaimer;
a heating section configured to heat the absorbent stored in the reclaimer and to which the alkaline agent has been mixed to obtain recovered vapor;
a second vapor cooler configured to cool the recovered vapor discharged from the reclaimer through a vapor line;
a first gas-liquid separator configured to separate a coexisting substance entrained in the cooled recovered vapor into recovered absorption agent vapor and a liquid coexisting substance by gas-liquid separation;
a cooler configured to cool the separated recovered absorption agent vapor;
a second gas-liquid separator configured to separate the recovered absorption agent vapor after cooling into a low-boiling point substance flue gas and a recovered absorbent by gas-liquid separation;
a heat exchanger configured to perform heat exchange of the liquid coexisting substance separated in the first gas-liquid separator with vapor condensed water from vapor supplied to the reclaimer to increase a temperature;
a CO2 absorber configured to bring the liquid coexisting substance after increase in the temperature and a CO2 gas in contact;
a second alkaline agent supply section configured to supply the alkaline agent to the liquid coexisting substance after absorption of CO2; and a distiller configured to distill the liquid coexisting substance to which the alkaline agent has been supplied while introducing the CO2 gas thereinto.
a reclaimer configured to introduce and store a part of an absorbent regenerated in an absorbent regenerator of a recovery unit that recovers CO2 or H2S in a gas;
a first alkaline agent supply section configured to supply an alkaline agent to the reclaimer;
a heating section configured to heat the absorbent stored in the reclaimer and to which the alkaline agent has been mixed to obtain recovered vapor;
a second vapor cooler configured to cool the recovered vapor discharged from the reclaimer through a vapor line;
a first gas-liquid separator configured to separate a coexisting substance entrained in the cooled recovered vapor into recovered absorption agent vapor and a liquid coexisting substance by gas-liquid separation;
a cooler configured to cool the separated recovered absorption agent vapor;
a second gas-liquid separator configured to separate the recovered absorption agent vapor after cooling into a low-boiling point substance flue gas and a recovered absorbent by gas-liquid separation;
a heat exchanger configured to perform heat exchange of the liquid coexisting substance separated in the first gas-liquid separator with vapor condensed water from vapor supplied to the reclaimer to increase a temperature;
a CO2 absorber configured to bring the liquid coexisting substance after increase in the temperature and a CO2 gas in contact;
a second alkaline agent supply section configured to supply the alkaline agent to the liquid coexisting substance after absorption of CO2; and a distiller configured to distill the liquid coexisting substance to which the alkaline agent has been supplied while introducing the CO2 gas thereinto.
4. The reclaiming device according to claim 3, wherein the second vapor cooler includes a first cooler configured to perform cooling with the liquid coexisting substance separated from the recovered vapor in the first gas-liquid separator by gas-liquid separation, a second cooler configured to perform cooling with reflux water from the absorbent regenerator, and a third cooler provided at a downstream side of a rich/lean solution heat exchanger disposed in a lean solution supply line, and configured to cool, with a rich solution, the recovered vapor after cooling with the second cooler.
5. The reclaiming device according to claim 3 or 4, comprising:
a CO2 gas introduction line configured to introduce the CO2 gas discharged from the CO2 absorber into the distiller; and a nitrogen supply section configured to introduce a nitrogen gas into the CO2 gas introduction line.
a CO2 gas introduction line configured to introduce the CO2 gas discharged from the CO2 absorber into the distiller; and a nitrogen supply section configured to introduce a nitrogen gas into the CO2 gas introduction line.
6. A reclaiming method comprising:
when recovering, in a reclaimer, a part of circulating absorbent that recovers CO2 or H2S in a flue gas in a CO2 or H2S recovery unit as recovered vapor, cooling the recovered vapor from the reclaimer, and then separating an entrained coexisting substance by gas-liquid separation to remove a liquid coexisting substance;
and introducing recovered absorption agent vapor after the gas-liquid separation into an absorbent regenerator.
when recovering, in a reclaimer, a part of circulating absorbent that recovers CO2 or H2S in a flue gas in a CO2 or H2S recovery unit as recovered vapor, cooling the recovered vapor from the reclaimer, and then separating an entrained coexisting substance by gas-liquid separation to remove a liquid coexisting substance;
and introducing recovered absorption agent vapor after the gas-liquid separation into an absorbent regenerator.
7. The reclaiming method according to claim 6, comprising:
cooling the recovered absorption agent vapor to obtain a liquid recovered absorbent in the introducing the recovered absorption agent vapor after separation into the absorbent regenerator;
heating the separated liquid coexisting substance, then bringing the liquid coexisting substance and a CO2 gas in contact, and then supplying an alkaline agent; and distilling, in a distiller, the liquid coexisting substance into which the alkaline agent has been supplied while introducing the CO2 gas thereto.
cooling the recovered absorption agent vapor to obtain a liquid recovered absorbent in the introducing the recovered absorption agent vapor after separation into the absorbent regenerator;
heating the separated liquid coexisting substance, then bringing the liquid coexisting substance and a CO2 gas in contact, and then supplying an alkaline agent; and distilling, in a distiller, the liquid coexisting substance into which the alkaline agent has been supplied while introducing the CO2 gas thereto.
8. The reclaiming method according to claim 7, wherein a nitrogen gas is added to the CO2 gas to be introduced into the distiller.
9. A recovery unit of CO2, H2S, or both of CO2 and H2S, comprising:
an absorber configured to bring a gas containing CO2, H2S, or both of CO2 and H2S and an absorbent in contact to remove CO2, H2S, or both of CO2 and H2S;
an absorbent regenerator configured to regenerate a solution that has absorbed CO2, H2S, or both of CO2 and H2S
to obtain the absorbent; and the reclaiming device according to any one of claims 1 to 5, configured to extract a part of the absorbent regenerated in the absorbent regenerator, and to remove a coexisting substance in the absorbent, wherein the absorbent regenerated in the absorbent regenerator is circulated and reused in the absorber, and recovered absorption agent vapor recovered from the reclaiming device is introduced into the absorbent regenerator.
an absorber configured to bring a gas containing CO2, H2S, or both of CO2 and H2S and an absorbent in contact to remove CO2, H2S, or both of CO2 and H2S;
an absorbent regenerator configured to regenerate a solution that has absorbed CO2, H2S, or both of CO2 and H2S
to obtain the absorbent; and the reclaiming device according to any one of claims 1 to 5, configured to extract a part of the absorbent regenerated in the absorbent regenerator, and to remove a coexisting substance in the absorbent, wherein the absorbent regenerated in the absorbent regenerator is circulated and reused in the absorber, and recovered absorption agent vapor recovered from the reclaiming device is introduced into the absorbent regenerator.
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JP2013-229324 | 2013-11-05 | ||
JP2013229324A JP5931834B2 (en) | 2013-11-05 | 2013-11-05 | Reclaiming apparatus and method, CO2 and / or H2S recovery apparatus |
PCT/JP2014/078110 WO2015068576A1 (en) | 2013-11-05 | 2014-10-22 | Reclaiming device and method and recovery device for co2, h2s, or both |
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CA2928613A1 true CA2928613A1 (en) | 2015-05-14 |
CA2928613C CA2928613C (en) | 2018-02-13 |
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EP (1) | EP3047893B1 (en) |
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CA (1) | CA2928613C (en) |
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JP6598688B2 (en) | 2016-01-14 | 2019-10-30 | 三菱重工エンジニアリング株式会社 | Acid gas recovery system and reclaiming apparatus used therefor |
CN107050912B (en) * | 2017-01-13 | 2022-08-02 | 陕西延长石油(集团)有限责任公司 | Gas-phase condensed liquid recovery system and method |
US11819777B2 (en) * | 2017-08-22 | 2023-11-21 | Saudi Arabian Oil Company | Systems and methods for enhancing amine agent recovery with a reclaimer |
JP6987597B2 (en) | 2017-10-20 | 2022-01-05 | 三菱重工エンジニアリング株式会社 | Reclaiming device and reclaiming method |
JP6998174B2 (en) * | 2017-10-20 | 2022-01-18 | 三菱重工エンジニアリング株式会社 | Acid gas removal device and acid gas removal method |
CN107754568B (en) * | 2017-11-28 | 2020-08-07 | 沈建冲 | Low-energy-consumption device for capturing and recovering carbon dioxide by flue gas and gas recovery process |
US10625199B2 (en) * | 2018-03-01 | 2020-04-21 | Mitsubishi Heavy Industries Engineering, Ltd. | CO2 recovery system and method of recovering CO2 |
FR3099710B1 (en) * | 2019-08-08 | 2021-08-06 | Ifp Energies Now | Absorption gas treatment process using thermally optimized hot flash solvent regeneration |
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JP3504674B2 (en) | 1992-03-03 | 2004-03-08 | 関西電力株式会社 | Method for removing carbon dioxide and sulfur oxides from flue gas |
JP4831833B2 (en) | 2007-03-28 | 2011-12-07 | 三菱重工業株式会社 | CO2 recovery device and waste treatment method in CO2 recovery device |
NO20092229L (en) * | 2009-06-09 | 2010-12-10 | Aker Clean Carbon As | Absorbent reclaimer |
WO2012067101A1 (en) * | 2010-11-16 | 2012-05-24 | バブコック日立株式会社 | Method and device for controlling system for chemically absorbing carbon dioxide |
JP5707894B2 (en) * | 2010-11-22 | 2015-04-30 | 株式会社Ihi | Carbon dioxide recovery method and recovery apparatus |
CA2858803A1 (en) * | 2011-12-14 | 2013-06-20 | Babcock-Hitachi Kabushiki Kaisha | Carbon dioxide chemical absorption system installed with vapor recompression equipment |
US9994512B2 (en) * | 2012-03-29 | 2018-06-12 | Htc Purenergy Inc. | System and process for reclaiming single and mixed amine solvents |
US9623366B2 (en) * | 2013-03-04 | 2017-04-18 | Mitsubishi Heavy Industries, Ltd. | CO2 recovery system and CO2 recovery method |
JP6071838B2 (en) * | 2013-10-18 | 2017-02-01 | 三菱重工業株式会社 | CO2 and / or H2S recovery apparatus and method |
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2013
- 2013-11-05 JP JP2013229324A patent/JP5931834B2/en active Active
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- 2014-10-22 EP EP14860438.2A patent/EP3047893B1/en active Active
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EP3047893A1 (en) | 2016-07-27 |
EP3047893B1 (en) | 2017-10-04 |
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US20160256825A1 (en) | 2016-09-08 |
JP5931834B2 (en) | 2016-06-08 |
AU2014344997A1 (en) | 2016-05-12 |
US10137415B2 (en) | 2018-11-27 |
CA2928613C (en) | 2018-02-13 |
EP3047893A4 (en) | 2016-10-19 |
WO2015068576A1 (en) | 2015-05-14 |
AU2014344997B2 (en) | 2017-05-25 |
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